Fluoride reprocessing of breeder fuels

ABSTRACT

SPENT FUEL OXIDE ARE FLUORINATED TO PRODUCE A PLUTONIUM-RICH STREAM AND A URANIUM-RICH STREAM. EACH STREAM IS COLD TRAPPED TO REMOVE HIGH BOILING FISSION PRODUCTS AND FED TO A THERMAL DECOMPOSER, VIA COMMON FEED POT WHICH ACTS AS A BATCH DISTILLER. FROM THE THERMAL DECOMPOSER, A PLUTOMIUM-RICH STREAM ISCOLD TRAPPED AND SENT TO A CONVERTER AND A URANIUM-RICH STREAM ISPURIFIED BY MEANS OF VARIOUS TRAPS AND DISTILLATION COLUMNS SENT TO THE CON-   VERTER IN THE CONVERTER, THE URANIUM-RICH STREAM AND PLUTONIUM-RICH STREAM ARE COMBINED AND CONVERTED TO MIXED PXIDES.

Aug. 2l, 1973 L.J. ANAsTAslA ET AL 3,753,920

FLUORIDE REPROCESSING OF BREEDER FUELS 2 Sheets-Sheet l Original Filed Oct. 24 1968 ug. 2l, 1973 .J. ANAsTAslA ET AL 3,753,920

FLUORIDE REPROCESSNG OF BREEDER FUELS 2 Sheets-Sheet 2 Original Filed Oct. 24, 1968 .uhhs S @l Env Nm Non JNM Now wb K N WN k uu .mi .A mm2 luik. QS@ mwi j m @bei Qu muf United States Patent O 3 753 920 FLUoRIDE REPRocEssmG oF BREEDER FUELS Louis J. Anastasia, Midlothian, Erwin L. Cai-ls, Glen Ellyn, Albert A. Chileiiskas, Chicago, Johan E. A.

3,753,920 Patented Aug. 2l, 1973 cce erate large quantities of plutonium While at the same time producing power. It is necessary to reprocess spent breeder fuel to separate the uranium and plutonium from fission products produced during irradiation. New processes are necessary for handling the new breeder fuels.

5 Graae, and Albert A. Jouke, Elmhurst, Nmlall M- A uoride volatility process has been developed at Levlfz, Bellwood Mam J' stemmer Park Forest Argonne National Laboratory for continuously reprocessand La Verne E. Trevorrow, Glen Ellyn, Ill., assignors ing spent breeder fuels. The object of this invention is to to the Umted States of America as represented by the r t ,d f I t d th 1 t United States Atomic Energy Commission dPrQCeSS Spell 9X1 e .115' 0 PTO 11C@ el er P l1 011111111 Continuation of abandoned application Ser. No. 770,145, 10 10x1de and Uranium d10X1 de Separately 01' nl lXed Prod- Oct. 24, 1968. This application Aug. 12, 1971, Ser. uctOf 23% plutonium dioxide-uranium dioxide with a No. 171,315 fission product decontairnnation factor of 10 to 107. The Int. Cl. C01g 43 06 decontamination factor is the ratio of the concentration of U-S. Cl. 252-301-1 R 2 Claims iission products in the spent fuel to the concentration of fission products in the product. The subject process is ABSTRACT 0F THE DISCLOSURE based on a plant capacity of about one metric ton actinides d t d t d e a 1uto per day, which is taken as the daily average discharge rate Spenj; fuel 0X1 es are urma? o pro uc p from a 15,000 megawatt electric network. Exact equip nimm'nch Stream and a urailmm'rfh Strem' Each Stream ment size and shape are influenced by heat balance and i2tstessimessagenastinessist 20 wggh w d; type o ue an t e extent o urnup. e process may e laaltlolsi gtlrsgrspll tgrgll eertrgsln better understood by reference to the following figures. verter and a uranium-rich stream is purified by means of BRIEF DESCRIPTION 0F THE DRAWINGS various traps and distillation columns and sent to the converter. In the converter, the uranium-rich stream and plu- 25 P IGS- and 2 represent a OWShee 0f the Process 0f tonium-rich stream are combined and converted to mixed the Inl/@m1011- oxides. DESCRIPTION OF THE PREFERRED w EMBODIMENT f a lication S.N. 770 145 now ab'alxse' cgrtuolg 30 With reference to the figures which represent a typical owsheet except for the broken lines at the gas coolers CONTRACTUAL ORIGIN 0F THE INVENTION and cold traps which represent batch operations, each The invention described herein was made in the course P1666 0f eqllllflleflt 1S labelled and numbered Where there of, or under, a contract with' the United Sta-tes Atomic are more than 011e 0f that Pa1t1c111a1 ype Table I 11SS the 35 number, size or capacity, construction material and op- Energy Commission. a

erating temperature for each piece of equipment. The BACKGROUND OF THE INVENTION reference numbers corresponding to each stream leaving This invention relates to a process for reprocessing or entering each piece of equipment are keyed to Table nuclear fuels and in particular to a nonaqueous process I I, which shows the actimde and iission product distribufor reprocessing fast breeder fuels. The next generation tion for the process as well as the gas ilow rate of each of nuclear reactors will be breeder reactors that will genstream.

TABLE i Number Construction Operating Equipment item required Size or capacity material temp., C.

A 1 Slab, 4" x 48 x 10 350 13302312355 2 Slab, 4" x 24" x 9'- 15 Cold trap, 1 ab nx 24" x 17 giidpvlbiriff .i- Staless stee1..-- 2 n 2 .10 Cold trap, 2 2 -80 t ...sa ivlfii gtgsaiiissi: I 1 mamme..- sername Waerme www 1. tat-eterna' Niets. 8.-- Tieernligl decomposer and uorinator 2 Slab; 4" X 31" Xl 10'. .do.. 350-500 NaF, 1 2 straps 1 3"diameterx4 0....-.. 350 31W solid waste container- 1 2 diameter x 9' Stainless steel Cold trap, 't x Zlfl" x 3'--. N kel 5.0. .m iscltniimcgl-ugu-u 1 Column, 4" diameter x 11' N30 Distillation column, 2 :go/111111121?, trdalaaeter x 29 gg me Idigimm traps, i Fiuia Bed (r. feminin. 2 1o" diameter x W2; .do Activated alumina trap, packed, 1 (TeFosorption) 1g, ddiaaigrxx 4% Copigr 6 N irifia as.; 2 wl; Gimme; Oxygen-hydrogen burn 1a 121 qdater X 6 StalllneSS Steel glrr gggrlgrstsfdl'.: 1 3 diameter x 12.5' (in Converter 1 2 x 2 x 10 Iuconel. 650 Sorber 1 5 diameter x 15 Mmm] TABLE II.GRAMS OF ELEMENT 0R COM1OUND Stream Flow rates (s.e.t.m.) 32. 7 2. 2

Stream Stream Flow rates (s.c.f.m.)- 23.0 2.0

Stream 31 31W 32 32W 33 33W 34 34W 35 Flow rates (s.c.f.m.)

After separation, the nonvolatile plutonium tetraiuoride is reiiuorinated in the fluorinator to plutonium hexauoride, purified and fed to a converter to produce the process product. The uranium hexauoride vapor leaving the thermal decomposer is passed through various sorbent traps and into a series of continuously operating distillation columns in which high and low boiling fission products are separated from the uranium hexafluoride. The bottoms from the last distillation column are passed through a second series of sorbent traps to further puriessentially all of the uranium and plutonium is converted fy the uranium hexauoride which is thereafter fed to to the volatile hexaliuorides along with some additional the converter with the plutonium hexauoride. formation of volatile fission product uorides. The over- The process will now be described in more detail, head Streams from reaCOrS A and B are Passed through particularly with reference to the drawings and Tables gas coolers and cold traps where the product actinides 1 and 1I,

are condensed. The product in the cold traps is liquefied Mechanical head-end and transferred to a common feed pot; subsequently the feed pot contents are volatilized to a thermal decom- Fuel elements or pins arriving at the reprocessing plant poser. In the decomposer, volatile plutonium hexafluoare removed from the shipping cask and tested for sodium ride is converted to nonvolatile plutonium tetrafluoride logging. Since product losses would occur by the introand separated from the volatile uranium hexaiiuoride. duction of sodium, those pins which are suspect must be set aside for further processing before they can be prepared for liourination. The sodium, in sodium-logged fuel pins, is converted to sodium oxide by exposure to a controlled air atmosphere during pin decladding. The oxide fuel is Washed with water to remove the sodium oxide as sodium hydroxide which is sent to waste. The

tion of many fission products occurs because nonvolatile fission product components are formed which stay with the alumina bed material and are eventually discharged to waste. Table III shows the separation of the actinide and fission product elements in terms of volatility of 142 -0 87. 5 (5) -0 398 d 6. 75(5) 1 223 l. 17(6) 8. 35(4) 2 95(3) 2 27(6) 1 01(3) EN() 2 77(3) 0.

69 6. 07(3) 43 2. 10(4) 7. 39 (6) 4. 49(4) Total. 9. 74 (5) 7. 55(6) 3. 70(4) B Grams of element. b Beta euries. 0 Assuming 100% conversion of beta plus gamma photons to heat. d Read 6.57 (5) as 6. 57)(105.

e Includes Ril-103 and Rh-l06.

f Not calculated. negligible.

R11-103 and 106 included with Ru.

sodium-free pins as well as the treated sodium-logged pins must be declad, and the fuel contained therein pulverized.

There are several methods which may be employed to declad the fuel pins. The pins may be scored longitudinally at two diametrically opposite points and then compressed by rollers to split the cladding into two fiat strips and release most of the fuel inside. Thereafter the strips may be rolled into spirals or chopped and vibrated to remove any oxide adhering thereto.

The pins may also 'be fed to a chopper to cut them into pieces approximately one-half to one inch long, The chopping is carried out -in a closed atmosphere because some fission product gases may be released which will be fed to the off-gas disposal system. The chopped pins are fed to a ball mill and then to a vibrating screen to separate the fuel from the cladding. After the cladding has been separated and the fuel pulverized, fuel is transported to a storage vessel while the cladding pieces are sent to waste disposal. If it is advantageous to oxidize the fuel prior to entry into the fluorination process, the ball mill operation may be carried out with an air or oxygen atmosphere. The oxide fuel powder which is -48 +100 mesh is mixed with alumina in a volume ratio of one part fuel to one-half part alumina and fed to a storage hopper with a capacity for an eight-hour load so that some inventory is always present. Mixing the fuel oxide with the alumina prior to storage reduces the volumetric heat load in the hopper. Mixed fuel oxide and alumina feeds from the storage hoppers to duorinator A.

Fuel fluorination The dimensions of fluorinator A are set out in Table I and the mixed fuel and alumina is fed into the iluorinator at the rate of 57 kg. per hour and iiuidized with a 23 v./o. fluorine in oxygen mixture at a ow rate of 37 standard cubic feet per minute, hereinafter s.c.f.m. The fluorination at 350 C. is selective in that uranium oxide, present as a mixture of uranium dioxide and U3O8, is converted to volatile uranium hexafiuoride, while plutonium dioxide is mainly converted to nonvolatile plutonium tetrafluoride. This Selective fluorination provides a primary separation which produces a plutonium-rich stream and a uraniumrich stream. In fluorinators A and B a basic decontamina- The table shows that about 49% of the fission product activity exists as nonvolatile fission product components that remain with the alumina.

The bottoms from fluorinator A, the composition of which is set out as stream 11 in Table II, are fed to the top stage of fluorinator B which is a two-stage reactor. The top stage of iiuorinator B is maintained at 500 C., while the bottom stage is maintained at 550 C. The solids flow from reactor A to reactor B is the same rate as that fed to reactor A so that the solid inventory in A is always maintained. Sirnilarly, the feed to reactor B is the same rate as the flow out of reactor B so that the fuel inventory in B is constant. The solids in reactor B which contains about 96% of the plutonium charged to reactor A in the form of plutonium tetraiiuoride are uidized with a v./o. fluorine-oxygen mixture. The two stages of fluorinator B are separated by, and the bottom is formed of, downwardly pointing truncated tetrahedrons which permit gas flow upward and solids flow downward. The countercurrent flow of solids and gas improves contact therebetween, and the truncated tetrahedrons simplify design b-y eliminating overflow pipes. The gas flow rate and the tetrahedrons are so designed to provide a residence time for the solids of 9 hours in the top stage and 9 hours in the bottom stage. Solids, which flow from the `bottom stage to waste `as stream 20W,.contain less than 1% of the charged plutonium, less than 1% of the charged uranium and the nonvolatile fission product uorides. The treatment of this and other solid waste streams will be later explained.

Purification The overhead stream 3 from iiuorinator A, as shown in the figures, feeds gas cooler 1 at a rate of 32.7 s.c.f.m. The composition of the overhead stream 3 is given in Table II and contains about 4% of the plutonium charged to the fluorinator as either hexauoride or oxyuorides, about 99% of the uranium, about one-half of the neptunium and most of the molybdenum, technetium, ruthenium, antimony and iodine. The cooler, as shown in Table I, is maintained at 15 C. and its principal purpose is to reduce the heat load to cold trap 1 and provide a first major separation of niobium and ruthenium pentafluorides. There are two gas coolers, one of which is always onstream, while the other is dumping to Waste.

The gas coolers are maintained above the dew point of the actinide hexafluorides and below the dew point of niobium pentafluoride and ruthenium pentafluoride in order to effect a primary separation thereof. As shown in Table II, essentially all of the ruthenium pentafluoride present is separated in gas cooler 1. Trace amounts of other ruthenium compounds present as ruthenium hexafluoride or ruthenium oxytetrafluoride are separated later in the process. About 80% of the niobium pentafluoride present is separated in gas cooler 1, as shown in Table II, while other niobium pentafluoride separation is provided in gas cooler 2. The overhead from gas cooler 1 feeds to cold trap 1 which is maintained at -80 C.

The cold traps are operated in pairs, one of which is always on-stream, While the other feeds to the feed pot, as shown in the figures. The cold traps principal purpose is to collect the volatile hexafluorides and to provide for the purge of non-condensable waste gases by means of a bleed stream 36 which has a continuous flow rate of 2.2 s.c.f.m. Bleed stream 36 contains all of the krypton and some xenon, tellurium hexafluoride, oxygen and fluorine, and minor amounts of other fission product fluorides. The process conditions favor formation of XeF4 and, although some xenon is discharged through streams 36 and 33W most of the xenon is separated as bottoms in the first distillation column. After the off-stream cold trap has been heated to about 80 C. under 2 atmospheres pressure and the liquefied product therein fed to the feed pot, the trap is blown down with fluorine which is recycled as stream to fluorinator A. As will be later explained, noncondensable gases from the plutonium fluorination cycle are also recycled to uorinator A so that bleed stream 36 is the only outlet for the noncondensable waste gases. This completes the first purification of the uranium-rich stream.

Overhead 12 from fluorinator B contains about 95% of the plutonium charged to reactor A, some uranium, about one-half of the neptunium, and minor amounts of other fission products and feeds into gas cooler 2 maintained at 10 C. There are two gas coolers 2 and they are operated in a similar manner to gas cooler 1, one is always on-stream, While the other is being flushed to waste. The purpose of gas cooler 2, like that of gas cooler 1, is to reduce the heat load to cold trap 2 and to effect a separation of the majority of the niobium and ruthenium pentafluorides present in stream 12. As shown in Table II, more than 95% of the niobium pentailuoride and more than 99% of the ruthenium pentafluoride present are separated in gas cooler 2 and sent to solid waste disposal as stream 12W. The noncondensed gases from gas cooler 2 flow to cold trap 2.

There are two cold traps 2, one of which is on-stream and maintained at 80 C., while the off-stream trap is being flushed to the feed pot. As may be seen from the figures, noncondensable gases from cold trap 2 are recycled as stream 30 to stream 10 and eventually are eliminated from the system in bleed stream 36. When cold trap 2 is taken off-stream, it is heated to about 80 C. under two atmospheres pressure and the liquefied product is fed to the feed pot. The cold trap is then blown down with fluorine which is passed through lithium fluoride trap A maintained at 450 C. and recycled to plutonium fluorinator B. Additional plutonium is added to stream 20, as plutonium hexafluoride desorbs from the lithium fluoride trap A, according to the following reaction:

The presence of plutonium in the lithium fluoride trap will be explained later in the process.

Stream 5 from cold trap 1 and stream 14 from cold trap 2, as liquids, are fed to the feed pot maintained at 80 C. under 2 atmospheres pressure, which effects a onestage batch distillation. There are two feed pots, one of which is on-stream, while the other is being blown down and then reloaded. The material in the feed pot on-stream, designated in Table II as stream 21, is evaporated from the pot as stream Z3 and fed to the decomposer and fluorinator along with a recycle stream 24 from cold trap 3. The make-up of the feed to the thermal decomposer is set out in Table II as stream 25. After the feed pot is taken off-stream about 1% of the actinide hexafluorides remain with considerable amounts of the dluorides of niobium, antimony and iodine. This heel 22 is blown down with fluorine and combined with overhead stream 27 from the thermal decomposer as a feed to a lithium fluoride trap B maintained at 300 C. A comparison of streams 21 and 23 shows the decontamination effected by the single-stage distillation from the feed pot.

There are two thermal decomposer-fluorinators, one of which is on-stream with the feed pot and acting as a thermal decomposer for the separation of plutonium and uranium, while the other is on-stream with cold trap 3 acting as a plutonium lfluorinator. The thermal decomposer consists of a fluidized bed of alumina maintained at 350 C. When stream 25 enters the thermal decomposer, the plutonium hexaiiluoride contained therein becomes unstable and decomposes to the nonvolatile tetrafluoride while the uranium hexafluoride remains stable and passes overhead. The overhead 27 from the thermal decomposer is fed to lithium fluoride trap B. When one thermal decomposer unit becomes loaded with plutonium tetrafluoride, stream 25 from the feed pot is switched from it to the other unit and the off-stream decomposer becomes a plutonium refluorinator. The fluorination in the off-stream thermal decomposer takes place at 500y to 550 C. with a diuidizing gas of -100% fluorine. The plutonium hexauoride produced in the refluorinator passes as stream 26 to cold trap 3 maintained at 80 C.

Cold trap 3` consists of three traps, one of which is always on-stream with the refluorinator, one of which is being warmed up to feed as stream 28 to the converter and one of which is being blown down and recycled as stream 24 to the thermal decomposer after it has fed to the converter. After the trap which has fed the converter is blown down, it is cooled in order to be ready to be put onstream with the refluorinator. Any noncondensables in cold trap 3 are recycled to the refluorinator and pass with the overhead 27 from the thermal decomposer to the distillation columns. Stream 2.8 represents the final purification of the plutonium-rich stream in this process and is fed into the converter for the conversion to the oxide; however, only about of the solid in cold trap 3 is vaporized to the converter. The other 10% is recycled to the thermal decomposer and provides decontamination factors of 2.5 103 for niobium pentailuoride and 1.7 102 for ruthenium pentafluoride.

Purification of the uranium-rich stream which is taken off as overhead 27 from the thermal decomposer and mixed with the blowndown heel Z2 from the feed pot starts with lithium fluoride trap B. As may be seen in Table II, stream 27 contains almost all of the uranium hexafluoride charged to the thermal decomposer and very little plutonium hexafluoride. Almost all of the fluorides of neptunium, molybdenum, technetium, tellurium and iodine pass with overhead 27. Lithium fluoride trap B, maintained at 300 C., sorbs any of the remaining unconverted plutonium hexafluoride from overhead 27 of the thermal decomposer as PuF4-4LiF.

Lithium fluoride trap B is operated in conjunction with lithium fluoride trap A. When trap B is taken off-stream from the thermal decomposer, it is heated to 450 C. and switched on-stream to fluorinator B. After lithium fluoride trap A is taken off-stream from -fluorinator B, it is cooled to 300 C. and put on-stream with the thermal decomposer. The lithium fluoride traps are continuously cycling, loading plutonium from the thermal decomposer and regenerating it t0 fluorinator B. The equipment specifications for the lithium fluoride traps are given in Table I.` Table IV sets out operating specications for the two traps.

TABLE IV Loading cycle:

Sizeinch dia. x 3.5 feet LiF--Low surface area -2 m.2/g., 45 kg. Operating temp- 300 C. PuFs load-2.8 kg. Loading time-2 days Gas flow rate2 s.c.f.m. `Gas residence time-4 sec. Regeneration cycle:

Operating temp-450 C. F2 rate-30 s.c.f.m. Regeneration time--1.6 days Ruthenium is built up on the lithium fluoride because some ruthenium is present in stream 29 and it does not desorb at 450 C. with a fiuorine purge. Periodic replacement of the lithium uoride trap material is necessary. Stream 31, which is now free of most of the plutonium hexauoride, feeds from lithium duoride trap 4B to sodium fluoride trap 1.

Sodium Iiuoride trap 1 is a uidized bed of sodium fiuoride particles about -48 `+100 mesh, maintained at 350 C. Since there are large amounts of fluorine present, this sodium fluoride trap does not sorb neptunium hexafluoride but does trap some of the ruthenium pentauoride, most of the niobium and antimony pentafluorides and virtually all of the residual plutonium hexauoride. This reduces the fission product activity and heat load in distillation column 1. There are two sodium fluoride traps, one always on-stream and one oftlstream; the contaminated olf-stream trap is dumped to solid waste disposal. Overhead 32 from the on-stream sodium [fluoride trap is fed to distillation column 1.

The principal purpose of distillation column 1 is to remove the high boilers, such as iodine pentauoride and xenon tetralluoride, from the process stream. As may be seen from stream 32W, essentially all the remaining niobium, ruthenium, antimony and iodine lluorides are removed and rejected to solid waste. The overhead 33 from distillation column 1, which is a 16stage column, operated at 75 C. and 2 atmospheres pressure, passes to a distillation column 2, which is a 23-stage column, operated at 80 C. and 2 atmospheres pressure. Uranium heX- auoride, technetium hexauoride, molybdenum hexauoride and tellurium hexauoride constitute most of the light fraction in the rst distillation column, but only .uranium hexauoride and technetium hexauoride become the heavy fraction in the second distillation column. Most of the molybdenum hexafiuoride and essentially all of the tellurium hexafluoride come olf the second distillation column as overhead 33W and are rejected to solid waste. The bottoms 34 from distillation column 2 are fed as a saturated vapor to a magnesium fluoride trap maintained at 125 C.

The magnesium lluoride trap sOrbs most of the technetium hexafluoride present in the steam, as well as most of the remaining molybdenum hexailuoride. There are two magnesium uoride traps and they are operated in a similar manner to the gas coolers previously described. The oit-stream magnesium fluoride trap is dumped as stream 34W to solid waste, while the process stream from the on-stream trap is fed to a combination sodium lluoride 2-UO2F2-sodium uoride 3 trap. The magnesium iluoride may be reused if desired by washing the oH-stream trap with water to purify the magnesium lluoride and thereafter drying prior to use.

The combination trap maintained at 350 C. sorbs most of the neptunium hexauoride present on the sodium fluoride while the fluorine present is reacted with the UOZFZ to form uranium hexauoride. The sorption of l0 neptunium hexauoride on sodium uoride produces uorine gas according to the following reaction:

TABLE V Grams compound Beta euries The converter, maintained at 650 C. is a bed of mixed plutonium-uranium oxides fluidized with a mixture of steam and hydrogen. Streams 28 and 3S feed the converter and are adjusted to give a 23% PuO2-UO2 product. Excess uranium hexafluoride from stream 35 is cold trapped and retained for further use, and excess hydrogen may tbe recycled to the waste gas disposal system, hereinafter explained. The converter operates in alternating periods, one hour with the hexauoride feed on and one hour with the hexauoride feed 01T. The oxide product remains in the reactor and the off-gas of hydrogen fluoride is fed to a limestone trap.

Minor ssion product species While the process has been described with the various fission products present as hexaor pentatluorides, some oxyuorides or other species may exist. As previously stated, besides ruthenium pentafiuoride, some ruthenium oxytetrafluoride and ruthenium hexafluoride may be present. Table VI shows the vapor pressures of these compounds compared to uranium hexauoride.

While most of the ruthenium pentatluoride condenses in gas cooler 1, little or no ruthenium oxytetrauoride or ruthenium hexauoride will condense in the gas cooler. These ruthenium compounds are transferred to the feed pot where the majority remain during the one-stage distillation to the thermal decomposer. Trace amounts of the ruthenium hexauoride and oxytetrafluoride pass to the thermal decomposer where ruthenium hexafluoride, which is unstable at 200 C., decomposes to the pentalluoride. Because of the large difference in volatilities at C., see Table VI, the pentafiuoride and oxytetrauoride are easily separated from the uranium-rich stream in distillation column 1 and pass with stream 32W to waste. Decontamination of the above-mentioned ruthenium compounds from the plutonium-rich stream takes place during the one-stage distillation from the feed pot, as shown in Table VII, and across the thermal decomposer. The botl1 toms or heel 22 from the feed pot is mixed with the uranium-rich stream 27.

TABLE Y II Percent Decontaminavolatilized tion factor Compound:

UF 99. NpFe..... 99.8 PuF..... 99.3 RuFa. 0. 08 1.25X10 RuOFi..- 5. 06 19. 7 RuFe-... 97.7 1.02

TABLE VIII CPS FPb-l :FP-2 Feed pot TID-1 Still 1 CT-3 RuFs.-.-. 3. 3)(10a 2. 5X104 1. 25)(10a 1)(103 1X10 2. 5X103 RuOF4.-- 1 1 20 1)(103 1X10 40 RuFu 1 1 (D) lDecomposed to RuFs.

In addition to molybdenum hexafluoride, some molybdenum oxytetrafluoride may be present. Table IX shows the pertinent vapor pressures at various temperatures.

b FP =gas cooler.

TABLE IX 80 C. 10 C. +15 C. +75 C.

Compound:

MoFa 0. 1 96. 2 358. 1 2. 870 10'5 0. 02 0. 20 10. 3 5X104 7. 44 55. 6 1. 592

As seen from the table, the bulk of the oxytetratluoride will condense in gas coolers 1 and 2. About half of the oxytetrafluoride present in the feed pot distills to the thermal decomposer and the other half passes with the feed pot heel 22 to be mixed with the uranium-rich stream 27. The molybdenum in the plutonium-rich stream is separated to a great extent in the one-stage distillation from cold trap 3, and as seen by the relative volatilities, the molybdenum in the uranium-rich stream remains as bottoms 32W in distillation column 1.

Besides technitium hexauoride some technetium oxytetrauode and some technetium trioxyfluoride may be present. Table X shows some of their respective vapor pressures.

TAB LE X Vapor pressure (mm. Hg)

As seen from Table X and the above discussions for ruthenium and molybdenum, the oxytetrauoride will condense in the gas coolers while the trioxyuoride and the hexafluoride transfer to the feed pot. The relative volatilities show that the hexauoride will follow uranium hexalluoride from the thermal decomposer and most of the oxytetrafluoride or trioxyfluoride will not distill from cold trap 3 with the plutonium hexalluoride. Any oxytetrauoride or trioxyuoride following the uranium-rich stream will remain as bottoms 32W in distillation column 1. The removal of technetium hexafluoride by the magnesium lluoride trap has been previously covered.

While some iodine oxypentauoride and iodine heptauoride may be present in the process stream, their volatilities at 80 C. are so large that a major separation will occur in cold traps 1 and 2, so these species will appear, if at all, in bleed stream 36.

Solid waste treatment The solid wastes from the process are alumina, discharged from the plutonium tluorinator, sodium fluoride from the sodium fluoride 1, 2, and 3 traps as well as from the Waste gas treatment, hereinafter explained, magnesium fluoride and lithium fluoride when it becomes unsuitable for use. These solid wastes generate large quantities of heat, thereby making their cooling and storage a problem. By mixing about 40% aluminum shot or powder with the solid waste, two-foot diameter storage cylinders may be used without exceeding 750 C. centerline temperatures. The aluminum melts due to the heat of the wastes and forms a superior heat transfer medium in the storage containers.

The sodium fluoride waste to be treated includes material from a fluid bed or sodium iluoride used with gas coolers 1 and 2. The ruthenium and niobium pentauorides from off-stream coolers 1 and 2 are blown out of the coolers with oxygen to a fluidized bed of sodium fluoride. When this trap is loaded, the trap material is dumped and added to the solid wastes described above, while the overhead oxygen is added to the process waste gases for disposal.

Gas waste treatment The gas wastes in the process consist of bleed stream 36, the bottoms from distillation column 1, the overhead from distillation column 2 and oxygen from the gas cooler clean-up described above. The overhead 33W from distillation column 2 is passed through a sodium fluoride trap, maintained at C., to remove molybdenum hexauoride and trace amounts of technetium hexai'luoride, uranium hexafluoride and tritium uoride. The overhead then passes through a packed bed of activated alumina, at 25 to 100 C., to remove tellurium hexauoride and trace amounts of fluorine and technetium hexauoride. Activated alumina is A1203 with a high surface area. The overhead 33W goes from the packed bed of activated alumina to a fluidized bed of activated alumina maintained at 500 C. Into this uidized bed are also fed the bottoms 32W from distillation column 1, the olf-gas 36 from the uorinators A and B and the oxygen used to ush gas coolers 1 and 2. The uorine is removed here and the gas continues on to a soda lime trap to remove iodine. In the soda lime trap, some tritium fluoride may be converted to tritium water. A molecular sieve dryer removes any tritium water present, and an oxygen burner converts the oxygen present to Water by combustion with hydrogen. The remaining gases are xenon and krypton which are compressed and stored for about thirty days prior to release to the stack.

The above description is of the preferred embodiment but, clearly, modifications may be made Within the scope of the invention. For instance, luorinator A may be operated at a temperature suicient to produce both uranium and plutanium hexafluoride; then, the overhead containing both actinide hexafluorides is passed through a gas cooler-cold trap series prior to introduction to the feed pot. There are numerous variations in conditions which may be applied to this process; however, the limitations of the process are only contained in the appended claims.

What we claim is:

1. A process for continuously processing spent nuclear fuel comprising: fiuorinating oxides of the spent fuel in a fluidized bed with a mixture of oxygen and uorine at about 350 C. to produce a gas rich in uranium hexauoride, tluorinating the remaining spent fuel in a uidized bed, maintained at between about 500 to 550 C., with a mixture of fluorine and oxygen containing a high proportion of lluorine to produce a gas rich in plutonium hexaluoride, separately removing most of the ruthenium pentauoride and niobium pentauoride from said gases by cooling the gases to between +15 C. and 10 C. and separating condensed fission products therefrom, combining said gases as a condensed gas and batch distilling the condensed gas to a thermal decomposer maintained at about 350 C., where a uranium rich stream passes overhead which carries most of the fission products present in the thermal decomposer and plutonium tetrauoride remain in the thermal decomposer, uorinating the plutonium tetrauoride in the thermal decomposer by passing fluorine gas upwardly therethrough at a temperature of about 500 C. to form a plutonium rich stream, decontaminating the uranium rich stream by passing it consecutively through a lithium uoride trap, a sodium fluoride trap, distillation columns to remove high low boiling fission product uorides, a magnesium iluon'de trap to remove technetium hexauoride and a combination sodium uoride-UOZFg-sodium fluoride trap whereby uorine gas and neptunium hexauoride are removed, removing residual niobium pentauoride and ruthenium pentauoride from the plutonium rich stream by condensing it at about 80 C. and converting the decontaminated uranium hexauoride and plutonium hexauoride to uranium dioxide and plutonium dioxide for reuse as nuclear fuel by passing both of these streams to a bed fluidized with steam and hydrogen to produce mixed 30 plutonium dioxide and uranium dioxide.

14 2. The process of claim 1 wherein said gases rich in uranium hexalluoride and plutonium hexauoride rst obtained are also condensed at about C. and the noncondensed gases are separated therefrom.

References Cited UNITED STATES PATENTS 3,294,493 12/ 1966 Jonke et al 423-19 2,875,021 2/ 1959 Brown et al 423-19 3,098,709 7/ 1963 Mecham et al 423-19 3,165,376 1/1965 Golliher 423-6 3,178,258 4/ 1965 Cathers et al 423-6 3,264,070 8/1966 Ramaswani et al 423-19 3,429,669 2/ 1969 Camozzo et al. 423-4 OTHER REFERENCES CARL D. QUARFORTH, Primary Examiner F. M. GITTES, Assistant Examiner U.S. Cl. X.R. 

